EP0449448A1 - Procédé pour la production d'un courant de produit enrichi avec de l'oxygène - Google Patents

Procédé pour la production d'un courant de produit enrichi avec de l'oxygène Download PDF

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Publication number
EP0449448A1
EP0449448A1 EP91302009A EP91302009A EP0449448A1 EP 0449448 A1 EP0449448 A1 EP 0449448A1 EP 91302009 A EP91302009 A EP 91302009A EP 91302009 A EP91302009 A EP 91302009A EP 0449448 A1 EP0449448 A1 EP 0449448A1
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Prior art keywords
column
gas
pressure
product
outlet
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EP91302009A
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German (de)
English (en)
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EP0449448B1 (fr
Inventor
Eiji Hirooka
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Linde LLC
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BOC Group Inc
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • B01D53/0476—Vacuum pressure swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • B01D53/0473—Rapid pressure swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B01D2253/108—Zeolites
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/30—Physical properties of adsorbents
    • B01D2253/302—Dimensions
    • B01D2253/304—Linear dimensions, e.g. particle shape, diameter
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/12—Oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/10—Single element gases other than halogens
    • B01D2257/102—Nitrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40035—Equalization
    • B01D2259/40037—Equalization with two sub-steps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40043—Purging
    • B01D2259/4005—Nature of purge gas
    • B01D2259/40052—Recycled product or process gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40058—Number of sequence steps, including sub-steps, per cycle
    • B01D2259/40066—Six
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/402—Further details for adsorption processes and devices using two beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • B01D53/053—Pressure swing adsorption with storage or buffer vessel

Definitions

  • This invention relates to a process for obtaining an oxygen enriched gas from a gas mixture containing principally oxygen and nitrogen as gas components, such as air, by means of pressure swing adsorption (PSA).
  • PSA pressure swing adsorption
  • Pressure swing adsorption systems and process have been widely used to produce oxygen enriched streams from mixed gases, including air, and a multitude of such systems and processes have been utilized.
  • Conventional vacuum PSA processes do produce a higher oxygen yield (50-60%) however the production rate is somewhat low.
  • the normal production rate of conventional three bed PSA processes is not particularly high; as an example, typically, the bed size factor is about 2000-2600 kg of zeolite per metric ton of oxygen produced per day.
  • an apparatus for carrying out the continuous production of an oxygen enriched stream of gas from a feed stream of air comprises two adsorption columns to cycle respectively said two adsorption columns between receiving said feed stream of air and producing said enriched oxygen stream, characterised by a vacuum pump, said vacuum pump being connected to both of said adsorption columns and adapted to withdraw gas continuously from one or the other of said adsorption columns during said repetitive cycle.
  • the system uses short cycle times to gain good usage of the sieve material but requires only two beds, thus greatly simplifying the prior three-bed processes that heretofore were needed for high yields.
  • one of the further features is the power saving by continuous operation of a vacuum pump with a two column system by simultaneously carrying out a equalization step supplying an oxygen enriched stream from the product to the outlet end of one column and a desorption to evacuate nitrogen rich gas from the inlet end of the same column.
  • the vacuum pump is run continuously throughout this step as well as the remaining steps. Since the vacuum pump is not running idle or unused during any step of the overall process, its use, and thus its power consumption, is optimized.
  • the two bed PSA process having high yield and production rate is achieved using relatively, fine particles of zeolite sieve material, such as 20-35 mesh size and even with larger particles such as 8-12 mesh size at short cycle times less than 30 seconds, preferably about 15-25 seconds.
  • the range of pressure swing uses vacuum for desorption less than 300 torr, preferably to 200 torr and maximum product pressure less than 5 psig and preferably less than 3 psig.
  • FIG. 1 and Figure 2 there is shown an apparatus for producing an enriched oxygen gas stream continuously generated from a gas containing principally oxygen and nitrogen, such as air.
  • a gas containing principally oxygen and nitrogen such as air.
  • Each of the two adsorption columns A and B contains an adsorbent capable of selectively adsorbing nitrogen.
  • the process is performed with relatively fine particles of zeolite of about 8-35 mesh, preferably about 12-20 mesh.
  • Typical zeolite sieve material is available from various zeolite manufacturers in the form of beads or pellets. Control of each of the steps can be regulated by conventional means, e.g., a timer to control solenoid operated valves of standard commercial design.
  • valves 1A and 2A are closed, thereby closing off the lower or inlet end of the first column A.
  • valves 4A and 5A are closed and valve 3A is open.
  • valves 9B and 10B are closed, thus gas from the outlet of column B is being introduced into the outlet of column A through valve 3A and the flow is controlled by valve 8B.
  • valve 6B is closed but valve 7B is open, thus gas is being withdrawn from the inlet end of column B by means of vacuum pump 16.
  • step 1 the pressure in column B which is initially higher than the pressure in column A is used to equalize the pressures in both columns, that is, column B may, at the beginning of step 1, be at a positive pressure of about 1010 torrs (4.84 psig) and is reduced to about 500 torrs (-5.03 psig) by the end of step 1 while column A commences step 1 at a pressure of about 260 torrs (-9.67 psig) and the pressure is raised to 470 torr (-5.61 psig). At the end of step 1, therefore, the column pressures are essentially equalized. Step 1 may take place extremely rapidly, and preferably from about 2 seconds to 6 seconds and more preferably in about 4 seconds.
  • Step 2 valve 3A is closed and valve 5A and valve 24 opened and oxygen enriched product gas from the reservoir 18 is introduced into the outlet of column A and is controlled by metering valve 26 to backfill column A and to raise the pressure further in column A.
  • the pressure in product reservoir is about 800 torr
  • the pressure within column A continues to increase from 470 torr (-5.61 psig) to about 660 torr (-1.93 psig).
  • gas is still being withdrawn from the inlet of column B through open valve 7B by vacuum pump 16 and the pressure within column B continues to decrease. That pressure may decrease, in step 2, from 500 torr (-5.03 psig) to about 450 torr (-6.00 psig).
  • the timing of step 2 is extremely rapid, preferably being from about 1 to 5 seconds, and more preferably about 3 seconds.
  • valve 1A is opened and air, or other feed gas containing principally oxygen and nitrogen under a predetermined feed pressure, is introduced to the inlet of column A.
  • Inlet pressures may vary but the inlet pressure should have a minimum predetermined pressure of between 3 and 7 psig, and preferably about 5 psig.
  • valve 5A is closed and valve 4A is opened, thus the feed air passes through column A where nitrogen is adsorbed and an oxygen enriched product stream passes from the outlet end of column A, through valve 4A, check valve 11 and through line 20 to the product reservoir 18.
  • the pressure in column A may increase from 660 torr (-1.93 psig) to about 1010 torr (4.84 psig) in producing oxygen enriched product.
  • step 3 gas continues to be withdrawn from the inlet end of column B to desorb or evacuate nitrogen enriched gas from column B by means of vacuum pump 16.
  • valve 10B is open and valve 24 open and oxygen enriched product stream is introduced into the outlet of column B to purge column B.
  • the flow of the oxygen enriched product stream is controlled by metering valve 26.
  • Step 3 is also carried out quite rapidly, in a range of cycle time preferably of about 10 seconds to 25 seconds and more preferably about 18 seconds.
  • step 4 equalization again takes place, this time by introducing the now higher pressure gas of column A into column B. That is carried out by closing valve 4A at the outlet of column A and opening valve 3A. At the outlet of column B, valve 10B is closed and thus, gas passes from column A to column B for equalization of pressures controlled by metering valve 8B. At the same time, of course, the feed stream is cut off by closing valve 1A at the inlet to column A and valve 2A is opened so that gas can be withdrawn from the inlet end of column A through vacuum pump 16. The inlet of column B is closed completely by closing valve 7B.
  • step 4 therefore, the pressures within column A and B are approximately equalized, the pressure in column A is reduced from about 1010 torr (4.84 psig) to about 500 torr (-5.03 psig) while the pressure in column B is increased from about 260 torr (-9.67 psig) to about 470 torr (-5.61).
  • Step 4 is carried out preferably in a time of from about 2 to about 6 seconds, and more preferably in about 4 seconds.
  • valve 3A is closed, thus closing entirely the outlet end of column A while gas continues to be withdrawn from the inlet end of column A drawing the pressure down, typically, from 500 torr (-5.03 psig) to a further 450 torr (-6.00 psig).
  • Valve 10B and 28 are opened and oxygen enriched product from product reservoir 18 enters column B to backfill that column controlled by metering valve 30 such that the pressure in column B is increased from, typically, about 470 torr (-5.61 psig) to about 660 torr (-1.93 psig).
  • the backfilling step takes place in from about 1 to 5 seconds, and preferably in about 3 seconds.
  • valve 6B is opened, thus introducing the pressurized feed stream into the inlet of column B.
  • Valve 9B is opened so that the oxygen enriched product stream from column B passes through check valve 12 and continues via line 20 to product reservoir 18.
  • valves 24 and 5A are opened to allow oxygen enriched gas to enter the outlet of column A to purge column A, controlled by metering valve 26.
  • gas continues to be withdrawn from the inlet of column A by vacuum pump 16 to desorb or evacuate nitrogen rich gas.
  • the pressure within column A decreases from about 450 torr (-6.00 psig) to about 260 torr (-9.67 psig) while the pressure in column B increases from about 660 torr (-1.93 psig) to about 1010 torr (4.84 psig).
  • the timing of step 6 can be from about 10 to about 25 seconds and preferably in about 18 seconds.
  • step 6 the entire sequence is repeated on a continual cyclic basis so that product is continuously taken from product reservoir 18 through valve 32 during each of the steps.
  • the vacuum pump 16 is also continuously utilized to withdraw gas alternatively, from one or the other of the two columns, thus it is efficiently utilized to minimize power use throughout the process.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Of Gases By Adsorption (AREA)
  • Oxygen, Ozone, And Oxides In General (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
EP91302009A 1990-03-29 1991-03-11 Procédé pour la production d'un courant de produit enrichi avec de l'oxygène Expired - Lifetime EP0449448B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US50145690A 1990-03-29 1990-03-29
US501456 1990-03-29

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Publication Number Publication Date
EP0449448A1 true EP0449448A1 (fr) 1991-10-02
EP0449448B1 EP0449448B1 (fr) 1997-01-22

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EP91302009A Expired - Lifetime EP0449448B1 (fr) 1990-03-29 1991-03-11 Procédé pour la production d'un courant de produit enrichi avec de l'oxygène

Country Status (14)

Country Link
US (1) US5122164A (fr)
EP (1) EP0449448B1 (fr)
JP (1) JP3091505B2 (fr)
KR (1) KR930006402B1 (fr)
CN (1) CN1028746C (fr)
AU (1) AU643513B2 (fr)
CA (1) CA2038510C (fr)
DE (1) DE69124276T2 (fr)
FI (1) FI95353C (fr)
IE (1) IE911045A1 (fr)
NO (1) NO177693C (fr)
NZ (1) NZ237529A (fr)
TR (1) TR25628A (fr)
ZA (1) ZA911907B (fr)

Cited By (7)

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US5328503A (en) * 1992-11-16 1994-07-12 Air Products And Chemicals, Inc. Adsorption process with mixed repressurization and purge/equalization
US5755856A (en) * 1995-03-02 1998-05-26 Sumitomo Seika Chemicals Co. Ltd. Process of recovering oxygen-enriched gas
DE19740848A1 (de) * 1997-09-17 1999-03-18 Sgi Prozess Technik Gmbh Druckwechselanlage zur Gewinnung von Sauerstoff aus der Luft und Verfahren zum Betrieb einer solchen
FR2776939A1 (fr) * 1998-04-07 1999-10-08 Air Liquide Procede de production d'oxygene par adsorption a variation de pression transatmospherique
US6641645B1 (en) 2002-06-13 2003-11-04 Air Products And Chemicals, Inc. Vacuum swing adsorption process with controlled waste gas withdrawal
FR3002160A1 (fr) * 2013-02-19 2014-08-22 Air Liquide Procede d'adsorption a pression alternee avec reservoirs de stockage combines
US12087519B2 (en) 2020-06-16 2024-09-10 Behr-Hella Thermocontrol Gmbh Operating unit for a vehicle

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HU176250B (en) * 1978-10-30 1981-01-28 Gyogyszerkutato Intezet Process for producing mikrobiologically 12-beta-hydroxycardenolide derivatives
US5268021A (en) * 1989-11-20 1993-12-07 Dynotec Corporation Fluid fractionator
US5156657A (en) * 1990-03-29 1992-10-20 The Boc Group, Inc. Process for pre-purification of air for separation
JP2981304B2 (ja) * 1991-05-13 1999-11-22 東洋エンジニアリング株式会社 ガス分離方法
JP2981302B2 (ja) * 1991-05-13 1999-11-22 東洋エンジニアリング株式会社 ガスの分離方法
US5340381A (en) * 1993-05-17 1994-08-23 Vorih Marc L Operating system for dual-sieve oxygen concentrators
WO1994028024A1 (fr) * 1993-06-01 1994-12-08 Enzon, Inc. Polymere modifie aux glucides presentant une activite erythropoïetique
JP3450885B2 (ja) * 1993-07-27 2003-09-29 住友精化株式会社 窒素富化ガス分離方法および装置
CA2133301A1 (fr) * 1993-10-06 1995-04-07 Ravi Kumar Methode d'adsorption par oscillation de la pression pour purifier une alimentation de melange gazeux sous haute pression, tenant compte du constituant le moins fortement adsorbe
US5429666A (en) * 1994-02-03 1995-07-04 Air Products And Chemicals, Inc. VSA adsorption process with continuous operation
US5540758A (en) * 1994-02-03 1996-07-30 Air Products And Chemicals, Inc. VSA adsorption process with feed/vacuum advance and provide purge
US5403385A (en) * 1994-02-08 1995-04-04 Alberta Research Council Serial flow pressure swing adsorption process for gas separation
US5411578A (en) * 1994-05-10 1995-05-02 Air Products And Chemicals, Inc. Vacuum swing adsorption process with mixed repressurization and provide product depressurization
JP3654661B2 (ja) * 1994-06-02 2005-06-02 大陽日酸株式会社 圧力変動吸着分離法による酸素発生方法
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FR2734171B1 (fr) * 1995-05-18 1997-12-26 Air Liquide Procede de production d'oxygene sous pression par adsorption
US5656067A (en) * 1996-02-23 1997-08-12 Air Products And Chemicals, Inc. VSA adsorption process with energy recovery
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FR2751244B1 (fr) * 1996-07-18 1998-09-04 Air Liquide Procede et installation de traitement d'un melange gazeux par adsorption a variation de pression
US5661987A (en) * 1996-10-25 1997-09-02 Pacific Consolidated Industries Three-bed nonimmobilized rapid pressure-swing adsorber
US5827358A (en) * 1996-11-08 1998-10-27 Impact Mst, Incorporation Rapid cycle pressure swing adsorption oxygen concentration method and apparatus
ATE261757T1 (de) * 1996-12-11 2004-04-15 Sgi Prozess Technik Gmbh Verfahren zum betrieb einer druckwechselanlage zur gewinnung von sauerstoff aus der luft
DE29719775U1 (de) * 1996-12-11 1998-02-05 SGI-Prozesstechnik GmbH, 63674 Altenstadt Druckwechselanlage zur Gewinnung von Sauerstoff aus der Luft
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US5871564A (en) * 1997-06-16 1999-02-16 Airsep Corp Pressure swing adsorption apparatus
FR2765491B1 (fr) * 1997-07-07 1999-08-06 Air Liquide Procede de separation d'un flux gazeux par un procede psa
FR2767717B1 (fr) * 1997-08-28 1999-10-01 Air Liquide Granulometrie et epaisseur de lit d'une unite psa
FR2769851B1 (fr) * 1997-10-21 1999-12-17 Air Liquide Installation de separation d'un melange de gaz
US6010555A (en) * 1997-11-04 2000-01-04 Praxair Technology, Inc. Vacuum pressure swing adsorption system and method
US6183537B1 (en) 1997-11-04 2001-02-06 Praxair Technology, Inc. Rotary blowers for pressure swing adsorption process and system
US6444014B1 (en) 1998-02-27 2002-09-03 Praxair Technology, Inc. VPSA process using adsorbent materials
US6500234B1 (en) 1998-02-27 2002-12-31 Praxair Technology, Inc. Rate-enhanced gas separation
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EP1085935B1 (fr) * 1998-02-27 2012-09-12 Praxair Technology, Inc. Separation de gaz plus rapide
FR2775619B1 (fr) * 1998-03-06 2001-04-20 Air Liquide Procede et installation de separation par adsorption d'un melange gazeux
FR2785553B1 (fr) * 1998-11-06 2000-12-22 Air Liquide Installation psa utilisant des vannes a durees de manoeuvre importantes et heterogenes
US6253778B1 (en) 1998-11-19 2001-07-03 Praxair Technology, Inc. Rotary valve
US6143056A (en) * 1998-11-19 2000-11-07 Praxair Technology, Inc. Rotary valve for two bed vacuum pressure swing absorption system
KR19990046799A (ko) * 1999-04-28 1999-07-05 조영옥 연소기의산소공급장치
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JP4301452B2 (ja) * 2003-02-18 2009-07-22 サンビオー２ カンパニー，リミティド 気体濃縮方法およびその装置
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US7591879B2 (en) * 2005-01-21 2009-09-22 Exxonmobil Research And Engineering Company Integration of rapid cycle pressure swing adsorption with refinery process units (hydroprocessing, hydrocracking, etc.)
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US7828878B2 (en) * 2006-12-15 2010-11-09 Praxair Technology, Inc. High frequency PSA process for gas separation
US20090205494A1 (en) * 2008-02-20 2009-08-20 Mcclain Michael S Single manifold assembly for oxygen-generating systems
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AU7371991A (en) 1991-10-03
FI95353B (fi) 1995-10-13
KR910016370A (ko) 1991-11-05
CN1056292A (zh) 1991-11-20
JPH04222613A (ja) 1992-08-12
ZA911907B (en) 1992-02-26
NO177693B (no) 1995-07-31
JP3091505B2 (ja) 2000-09-25
CN1028746C (zh) 1995-06-07
CA2038510C (fr) 2000-11-21
AU643513B2 (en) 1993-11-18
KR930006402B1 (ko) 1993-07-14
NO911084L (no) 1991-09-30
CA2038510A1 (fr) 1991-09-30
US5122164A (en) 1992-06-16
FI95353C (fi) 1996-01-25
DE69124276T2 (de) 1997-05-07
NO911084D0 (no) 1991-03-19
NO177693C (no) 1995-11-08
IE911045A1 (en) 1991-10-09
FI911558A0 (fi) 1991-03-28
FI911558A (fi) 1991-09-30
DE69124276D1 (de) 1997-03-06
TR25628A (tr) 1993-07-01
EP0449448B1 (fr) 1997-01-22
NZ237529A (en) 1992-10-28

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